Polymerization of olefins

ABSTRACT

The present invention relates to the method of polymerizing olefinic monomers utilizing a solid catalyst composition comprising a solid catalytic complex and an activator, to the resultant high impact resistant polymers, to the method of making such catalytic complex, and to the catalytic complex; said catalytic complex comprising the reaction product of an organic oxygenated compound of a metal of groups Ia, IIa, IIb, IIIb, IVb, VIIa, and VIII of the Periodic Table, an organic oxygenated transition compound of a transition metal of groups IVa, Va, and VIa of the Periodic Table, and an aluminium halide.

United States Patent [191 Berger et a1.

[ Aug. 26, 1975 POLYMERIZATION OF OLEFINS Inventors: Eugene Berger; Jean-Louis Derroitte, both of Brussels, Belgium Assignee: Solvay & Cie, Brussels, Belgium Filed: Dec. 6, 1972 Appl. No.: 312,744

Foreign Application Priority Data Dec. 8, 1971 Luxembourg 64420 June 1, 1972 Luxembourg 65445 U.S. Cl 260/882 R; 260/882 B; 260/93];

260/949 DA; 260/949 E Int. Cl. COSf 1/42 Field of Search 260/882 R, 94.9 DA, 94.9 E

7/1972 Diedrich et al. 260/949 DA 8/1972 Jones 260/949 E 3,718,636 2/1973 Stevens et al. 260/949 DA FOREIGN PATENTS OR APPLICATIONS 7,1 13,010 4/1972 Netherlands 260/949 DA Primary Examiner-Joseph L. Schofer Assistant Examiner-A. Holler Attorney, Agent, or FirmPennie & Edmonds [57] ABSTRACT The present invention relates to the method of polymerizing olefinic monomers utilizing a solid catalyst composition comprising a solid catalytic complex and an activator, to the resultant high impact resistant polymers, to the method of making such catalytic complex, and to the catalytic complex; said catalytic complex comprising the reaction product of an organic oxygenated compound of a metal of groups la, Ila, llb, illb, lVb, Vila, and VIII of the Periodic Table, an organic oxygenated transition compound of a transition metal of groups IVa, Va, and Vla of the Periodic Table, and an aluminium halide.

15 Claims, No Drawings POLYMERIZATION ()F OLEFINS BACKGROUND OF THE IN\ ENTION It is known that one can use for the lint-pressure polymcrization of olefins catalytic systems containing a compound ofa transition metal and an organo-mctallic compound.

It is also known frotn Belgian Pat. No. 705.210 that one can use as compound of the transition metal of the catalytic systems mentioned above a solid obtained by reacting a halogenated compound of a transition metal with an oxygenated compound of a divalent metal such as magnesium. The catalytic systems thus obtained are very active if they are compared with those in which the halogenated compound ofa transition metal is used as it is.

In Belgian Pat. No. 767.586. catalytic systems are described. one of the components of which is prepared by reacting an organic oxygenated compound of a divalent metal with an alkylaluminium halide. separating the product of this reaction and reacting it then with a halogenated compound of a transition metal. These cata lytic systems are also characterized by a high activity.

However. such catalytic systems with a high activity and others of the prior art lead to polymers which have an important defect. In point of fact. while their physical properties and more particularly their mechanical properties are on the whole quite satisfactory. their resistance to impact is sometimes insufficient. Now. the resistance to impact is an essential quality for polyolet'ins because they are used mainly for manufacturing objects which are used for handling (crates. tanks. pallets) and packing (bottles. films) which are subject to impact when they are used.

SUMMARY OF THE INVENTION It has now been found that the use of a new type of catalytic complex for the low-pressure polymerization of olclins makes it possible to manufacture. with very high activities, polyoletins which possess a very good resistance to impact.

The present invention relates to the method of polymerizing olefinic monomers utilizing a solid catalyst composition comprising a solid catalytic complex and an activator. to the resultant high impact resistant polymers. to the method of making such catalytic complex, and to the catalytic complex: said catalytic complex comprising the reaction product of an organic oxygen ated compound of a metal of groups la. Ila. llb. lllb. lVb. Vlla. and VIII of the Periodic Table. an organic oxygenated transition compound of a transition metal of groups IVa. Va and Vla of the Periodic Table. and an aluminum halide.

DETAILED DESCRIPTION The solid catalytic complexes of the present invention are prepared from organic oxygenated compounds of metals of Groups Ia, Ila. IIb, IIIb. lVb. VIIa and VIII of the Periodic Table. Among these metals one may mention by way ofexample lithium. sodium. potassium. magnesium. calcium. zinc. boron. aluminum. silicon. tin. manganese. iron. cobalt and nickel. However. it is preferable to use organic oxygenated compounds of divalent metals such as magnesium. calcium. zinc. man ganese. iron. nickel. cobalt. tin and the like. Good results are also obtained with organic oxygenated com pounds of aluminum and silicon. The best results are obtained with the oxygenated organic compounds of magnesium and these are preferred. As used herein the term "oxygenated organic compounds" is intended to mean all the compounds in which any organic radical is attached to the metal via oxygen; that is to say. compounds containing at least one sequence of metaloxygen-organic radical bonds per atom of metal. The best results are obtained when the metallic bonds of the organic oxygenated compounds only comprise sequcn ces of metal-oxygcn-organic radical bonds.

However. the organic oxygenated compounds used in the invention may contain. in addition to the organic radicals attached to the metal via oxygen. other radi cals but to the exclusion of halide radicals. that is to say the fluoride. chloride. bromide and iodide radicals. These other radicals are preferably oxygen and the inorganic radicals attached to the metal via oxygen such as the OH. (SO.)t NO;,. (PO -(CO;,) and -CIO radicals. They may also be organic radicals attached directly to the metal by carbon.

The organic radicals attached to the metal via oxygen are of any type. They are selected preferably from among the radicals containing 1 to 20 carbon atoms and more particularly from among those containing 1 to 6 carbon atoms. These radicals may be saturated or unsaturated. with branched chains. straight chains or cyclic; they may also be substituted and/or contain hetero atoms such as O. S. N. P in their chain. They are selected in particular from among the alkyl. alkenyl. aryl. cycloalkyl. arylalkyl. alkylaryl. acyl. aroyl radicals and their substituted derivatives.

Among the organic oxygenated compounds which can be used within the scope of the invention. one may mention:

I. The alkoxides such as methylatcs. ethylates. isopropylates. n-butylates. isobutylatcs. methoxyethylatcs and hydroxymcthylates'.

2. phenatcs such as salts of phenic acid. naphthenates. anthraccnates. phcnanthrcnates and crcsolatcs;

3. the salts of carboxylic acids such as acetates. butanoates. Iaurates. pivalates. crotonatcs. phenylacctatcs. benzoates. malonates. adipates. sebacates. phthalates. mellitates. acrylates. olcates and maleates'.

4. the chelates (that is to say organic oxygenated compounds in which the metal possesses at least one sequence of normal bonds of the metal-oxygemorganic radical type and at least one coordination bond so as to form a hctcrocycle in which the metal is included). such as the enolatcs and in particular the acetyl acetonates as well as the complexes obtained from phenolic derivatives possessing an electron donor group in the ortho position in relation to the hydroxyl group and in particular the complexes of B-hydroxyquinolcin; and

5. the organic nitrogenated oxygenated compounds (that is to say compounds containing sequences of metal-oxygen-nitrogen-organic radical bonds) such as the oximates and in particular butyloximates. dimethylglyoximates and cyclohexyloximates. the salts of hydroxamic acids and the salts of hydroxylamines and in particular the derivatives of Nmitroso-N-phenylhydroxylamine.

However. it is preferable to use alkoxides and phenates and more particularly those derived from divalent metals (preferably magnesium) which only possess sequences of divalent metal-oxygen-organic radical bonds.

The use of the organic oxygenated compounds containing several different organic radicals also falls 3 within the scope of the invention. The same applies to the use of a number of different organic oxygenated compounds of one and the same metal.

Likewise one may use several organic oxygenated compounds of different metals. in this case. these compounds may be used in the form of mixed complex compounds or again scperately. A particularly advantageous form of embodiment of the invention consists in using jointly an organic oxygenated compound of a metal of Group lIa (preferably magnesium) and an organic oxygenated compound of a metal of groups lllb and Nb (preferably silicon and more particularly aluminium).

In order to prepare the catalytic complexes used in the invention one also uses organic oxygenated transition compounds of transition metals of groups lVa. Va and Vla of the Periodic Table.

Among these metals it is preferred to use titanium, zirconium and vanadium. The best results are obtained with titanium.

By organic oxygenated transition compounds as such term is used herein. it is intended to mean compounds in which an organic radical is attached to the transition metal via oxygen. The compounds containing other radicals than the organic radicals attached to the transition metal via oxygen and in particular compounds containing halide radicals (fluoride. chloride. bromide and iodide) are excluded from the scope of the present invention. However. compounds containing metal-oxygen bonds and condensed compounds containing sequences of metal-oxygen-mctal bonds may also be used provided they have at least one sequence of mctal-oxygen-organic radical bonds per molecule.

The organic radicals attached to the transition metal via oxygen may be of any kind. They generally comprise from I to carbon atoms and preferably 1 to ID carbon atoms. The best results are obtained when they contain l to 6 carbon atoms. The organic radicals are preferably selected from among the hydrocarbon radicals and particularly from among the alkyl radicals (linear or branched). cycloalkyl radicals. arylalkyl radicals. aryl radicals and alkylaryl radicals.

The organic oxygenated transition compounds are represented by the general formula [Tr O (OR),,],, in which Tr is a transition metal of groups lVa. Va and Vla ofthe Periodic Table. in which R is an organic radical as defined above. in which .r and y are any numbers such that x 2 0 and y 0 and are compatible with the valency of the transition metal and in which m is an intcger. It is preferable to use organic oxygenated transition compounds in which .r is such that 0 s .r s l and m is such that l Sm 56.

Among the organic oxygenated transition compounds which can be used within the scope of the present invention. one may mention:

2. the phenatcs such as Ti(OC,;H

3. the oxyalkoxides such as VO(OiC H;)-.,;

4. the condensed alkoxidcs such as Ti O(OiC;,H and 5. the enolatcs such as titanium acetylacctonate.

The use of organic oxygenated transition compounds containing several different organic radicals also falls within the scope of the present invention. The same applies to the use of several different organic oxygenated transition compounds of one and the same transition 4 metal and the use of a number of organic oxygenated transition compounds of different metals.

The third component used for preparing the catalytic complexes is an aluminium halide. Onc preferably chooses it from among the halides of aluminium of the general formula AIR ,,R;,.,, in which R is a hydrocarbon radical containing 1 to 20 carbon atoms and preferably l to 6 carbon atoms. R' is a halide which may be fluo ride. chloride. bromide or iodide and n is any number such that 0 g n 3. Preferably R is selected from among the alkyl (linear or branched). cycloalkyl. arylalkyl. aryl and alkylaryl radicals. The best results are obtained when R represents chlorine and n is such that 0 s n s 2 and preferably such that l s n s 2.

Examples of preferred halides of aluminum which can be used in the invention are AlCl Al(C H,-.)Cl Al (C ,H Cl and Al(C H Cl.

One may also use any number of other aluminium halides.

In order to carry out the reaction of the formation of the complex. the organic oxygenated compound. the organic oxygenated transition compound and the aluminium halide may be used in the solid state. for example in suspension in an inert diluent or in the form of dry particles; in the liquid state. when the conditions of operation permit it; in the form ofa solution; and in the form of a vapor or gas.

It is preferable to carry out the reaction of the formation of the solid complex in a liquid medium. In order to do this. the reaction can be carried out in the presence of a diluent. In such case the diluent selected is preferably one in which at least one of the reagents is soluble. Any of the solvents usually used in organic chemistry may be employed. However. it is preferable to use alkanes and cycloalkanes containing from 4 to 20 carbon atoms. such as isobutane. normal pentane. normal hexane. cyclohcxanc. methyleyclohexane and the dodecanes. One may also use the alcohols containing 1 to [2 carbon atoms per hydroxyl group. such as ethanol. butanol and cyclohexanol. When a diluent is used. it is preferable for the total concentration of the dissolved reagent or reagents to be greater than 5 percent by weight and preferably greater than 20 per cent by weight. based on the weight of the diluent.

The reaction can also be carried out in a liquid medium in the absence of diluent. and this constitutes a preferred mode of embodiment of the invention. by choosing conditions of temperature and pressure such that at least one of the reagents is in the liquid state. Preferably one operates under conditions such that the organic oxygenated transition compound is liquid. In practice. it frequently happens that this organic oxygenated transition compound when maintained in the liquid state is capable of dissolving the organic oxygenated compound. One may also use a second organic oxygenated compound which is liquid and capable of dissolving the former.

The temperature at which the reaction is carried out is not critical. It is generally chosen such that at least one of the reagents is liquid or dissolved. For reasons of convenience. it is preferable to operate at between 20 and 300C and more particularly between 50 and 200C. The pressure is also not critical; one generally operates in the vicinity of atmospheric pressure. So as to favor the homogenization of the reaction medium one generally agitatcs the medium during the period of reaction.

The order of addition of the reagents may be as desired. However. it is preferable to operate by one of the following methods:

l. The organic oxygenated compound is brought into contact with the organic oxygenated transition compound by adding one to the other or by mixing them gradually. ln practice it frequently happens that in this way a complex is formed which is liquid or soluble in the diluent. The aluminum halide is then gradually added.

2. The organic oxygenated transition compound and the aluminium halide are mixed (preferably rapidly) and then the organic oxygenated compound is added.

3. The three reagents are simultaneously and gradually mixed together. The speed of addition of the reagents is also not critical. It is generally chosed so as not to bring about an abrupt heating of the reaction medium due to the rapid rate of reaction. The reaction may be carried out continuously or discontinuously.

The quantities of organic oxygenated compound, organic oxygenated transition compound and aluminium halide to be preferably used are stated below.

The quantity of the organic oxygenated transistion compound or compounds to be used is defined in relation to the total quantity of the organic oxygenated compound or compounds used. it may vary within wide limits. Generally speaking it is between 0.01 and 10 gram atoms of transition metal present in the organic oxygenated transition compound per gram atom of metal present in the organic oxygenated compound. It has been observed that the productivity of the catalytic complexes of this invention. that is to say the quantity of polymer produced in relation to the quantity of catalytic complex used is maximal when one uses a ratio of between 0.05 and 5 gram atoms of transition metal in the transition compound per gram atom of metal in the oxygenated compound. The best results are obtained when this ratio varies between 0. l and 2 gram atoms per gram atom. However. when the ratio varies between 0.025 and 0.10 gram atoms per gram atom the specific activity. that is to say the quantity of polymer produced in relation to the quantity of transition metal in the transition compound. is extremely high; on the other hand. the productivity is lower.

The quantity of aluminium halide to be used. reckoned in relation to the total quantity of the organic oxy- .genated compound or compounds and of the organic oxygenated transition compound or compounds used. may also vary within wide limits. Generally speaking it is between 0.10 and 10 moles of aluminium halide per grant equivalent of metal and transition metal present in all of the organic oxygenated and organic oxygenated transition compounds used. By gram equivalent one means the weight in grams ofthese metals which is capable of reacting with or replacing one gram atom of hydrogen. Preferably this quantity is between 0.50 and 5 moles per gram equivalent. The best results are obtained when it is between 0.75 and 2 moles per gram equivalent.

When one uses the variant of the invention in which there is used an organic oxygenated compound of a metal A of Group Ila and a second organic oxygenated compound of a metal B of Groups lllb and lVb. the quantities ofthesc compounds to be used are such that the ratio between the quantity of metal A and that of the metal B is between 0.0l and I00 gram atoms per gram atom. Preferably this ratio is between 0.1 and gram atoms per gram atom. The best results are obtaincd when it is between 0.5 and l.5 gram atoms per gram atom.

The catalytic complexes prepared in accordance with the invention are solid. They are insoluble in the solvents. such as alkanes and eycloalkanes which can be used as diluents. They maybe used in polymerization in the form in which they are obtained. without being separated from the reaction medium. However. it is preferable to separate them from this reaction medium by any of the known usual means. When the reaction medium is liquid. one may use. for example. filtration. dc cantation or centrifuging.

After separation. the catalytic complexes may be washed so as to eliminate excess reagents with which they may still be impregnated. For this washing one uses any inert diluent and for example those which can be used as constituents of the reaction medium such as the alkanes and cycloalkancs. After washing. the catalytic complexes maybe dried. forexamplc. by sweeping them with a stream of dry nitrogen or in vacuo.

The mechanism of the reaction of the formation of the catalytic complexes of the invention is not known. The elemental analysis of the catalytic complexes after separation and washing shows that they are chemically combined complexes. products of chemical reactions. and not the result of mixtures or adsorption phenomena. ln point of fact it is impossible to dissociate one or other of the constituents of these complexes using purely physical means of separation.

The catalytic complexes of the invention. the exact nature of which is also not well known. contain metal. transition metal. aluminium and halogen in variable quantities. More often than not they contain. per kg. between [0 and g of metal from the organic oxygenated compound or compounds. between 20 and 250 g oftransition metal. more than l0 g of aluminium and between 200 and 700 g of halogen. They are characterized by a high specific surface area. more often than not greater than 50 sq.m. per gram and which may go up as far as figures as high as 300 to 400 sq.m. per gram.

The catalytic compositions according to the invention also comprise an organic compound which serves as activator. One uses the organic compounds of metals of Groups la. lla. llb. lllb and [Vb of the Periodic Table such as the organic compounds oflithium. magnesium. zinc. aluminium and tin. The best results are obtained with the organic compounds of aluminium.

It is possible to use completely alkylated compounds whose alkyl chain contains from I to 20 carbon atoms and are straight or branched. such as for example 11 butyl lithium. dicthyl magnesium. dicthyl zinc. trimethyl aluminium. triethyl aluminium. triisobutyl aluminium. tri-n-butyl aluminium. tri-n-decyl aluminium. tetraethyl tin and tetrabutyl tin. However. it is preferable to use the trialkyl aluminiums whose alkyl chains contain from 1 to 10 carbon atoms and are either straight or branched.

It is also possible to use the alkyl metal hydrides in which the alkyl radicals also contain from I to 20 carbon atoms. such as di-isobutyl aluminium hydride and trimethyl tin hydride. Also suitable are the alkyl halides of metals in which the alkyl radicals also contain from I to 20 carbon atoms such as ethyl aluminium sesquichloride. dicthyl aluminium chloride and diisobutyl aluminium chloride.

Finally it is also possible to use organo-aluminium compounds obtained by reacting trialkyl aluminium or 7 dialkyl aluminium hydrides whose radicals contain from 1 to 20 carbon atoms with diolefins containing 4 to 20 carbon atoms, and more particularly the compounds known as isoprenyl aluminiums.

The process of the invention is applied to the poly merization of olefins with a terminal unsaturation whose molecule contains from 2 to 20. and preferably 2 to 6. carbon atoms, such as the a-olefins ethylene. propylene. butene-l 4-methylpentene-l and hexcne-l. It also applies to the copolymerization of these olefins with one another as well as with diolefms preferably containing 4 to 20 carbon atoms. These diolefins may be unconjugated aliphatic diolefins such as hexadiene 1,4.monocyclic diolefins such as 4-vinylcyclohexene. 1.3-divinyl-cyclohexane. cyclopentadiene or cyclooetadiene-1.5. alieyclic diolefins having an endocyclic bridge such as dicyclopentadiene or norbornadiene and conjugated aliphatic diolefins such as butadiene and isoprene.

The process of the invention is applied particularly well to the manufacture of homopolymcrs of ethylene and copolymers containing at least 90 moles% and preferably 95 moles% of ethylene.

The polymerization may be carried out by any known process such as in solution, or in suspension in a solvent or hydrocarbon diluent. or again in the gaseous phase. For processes in solution or in suspension one uses solvents or diluents analagous to those used for the preparation of the catalytic complex; preferably. alkanes or cycloalkanes such as butane, pentane, hexane. heptane. cyclohexane. methylcyclohexane or mixtures thereof. One may also carry out the polymerization in the monomer or one of the monomers maintained in the liquid state.

The polymerization pressure is generally between atmospheric pressure and 100 kg/cm preferably 50 kglcm The temperature is generally selected between 20 and 200C and preferably between 60 and 120C. The polymerization may be carried out continously or discontinuously.

The organo-metallic compound and the catalytic complex may be added separately to the polymerization medium. Also, one may bring them into contact at a temperature between 40 and 80C over a period ranging up to 2 hours before introducing them into the polymerization reactor. They can also be brought into contact with one another in several stages or again one may add one part of the organo-metallic compound before the reactor or again one may add several different organo-metallic compounds.

The total quantity oforgano-metallic compound used is not critical; it is generally between 0.02 and 50 mmoles per dm of solvent, diluent or reactor volume and preferably between 0.2 and 5 mmoles per dm".

The quantity of catalytic complex used is determined according to the transition metal content of the catalytic complex. It is generally chosen so that the concentration is between 0.0()l and 2.5 and preferably between 0.01 and 0.25 m. gram atoms of metal per drn of solvent. diluent or reactor volume.

The ratio of the quantities of organo-metallic compound and catalytic complex is also not critical. It is generally chosen so that the ratio of organo-mctallic compound/transition metal expressed in mole/gram atom is greater than 1 and preferably greater than 10.

The mean molecular weight based on the melt index of the polymers manufactured according to the process ofthe invention may be regulated by the addition to the 8 polymerization medium of one or more molecular weight modifiers such as hydrogen. zinc. or diethyl cadmium, alcohols or carbon dioxide.

The specific gravity of the homopolymers produced according to the process of the invention can also be regulated by the addition to the polymerization medium of an alkoxide of a metal of groups Na and Va of the Periodic Table. Thus one may produce polyethylenes with a specific gravity intermediate between that of the polyethylcnes manufactured by a high-pressure process and that of the classic high-density polyethylenes.

Among the alkoxides which are suitable for this regulation. those of titanium and vanadium whose radicals contain 1 to 20 carbon atoms each are particularly ef fective. One may mention among them Ti(OCH Ti- (OC.,H Ti[OCH CH(CH;.) Ti(OC..H, and Tilfi 33 -1.

The process of the invention makes it possible to produce polyolefins with remarkably high productivities. Thus in the homopolymerization of ethylene. the productivity expressed in grams of polyethylene per gram of catalytic complex used usually exceeds 10.000 and in many cases 20.000. The activity reckoned on the quantity of transition metal present in the catalytic complex is also very high. In the homopolymerization of ethylene also. expressed in grams of polyethylene per gram of transition metal used. it regularly exceeds 50.000 and in many cases 100.000. [n the most favorable cases it is greater than 1.000.000.

For this reason. the content of catalytic residues of the polymers produced according to the process of the invention is extremely low. More particularly. the residual content of transition metal is extremely low. It is the derivatives of transition metals which are troublesome in the catalytic residues because of the colored complexes which they form with the phenolic antioxidants usually employed in polyolcfins. That is why. in the classic processes for the polymerization of olefins by means of catalysts containing a transition metal compound, the polymers have to be purified to remove the catalytic residues which they contain. for example by a treatment with alcohol. In the process of the inven tion. the content of troublesome residues is so low that one may dispense with the purification treatment which is a costly operation in terms of raw materials. time. and capital.

The polyolefins produced according to the invention are characterized by a remarkably high resistance to impact. Thus the homopolymers of the ethylene manufactured according to the invention. when their melt index is about 5. possess a resistance to impact measured by the Izod test of at least about 10 kg cm/cm notch. The polyethylenes of the same melt index manufactured by means of high-activity catalytic systems of prior art do not have a resistance impact measured according to the same test which is greater than approximately 6 kg cm/cm notch.

The polyolefins obtained by the process of the invention may be used according to all known fabricating techniques such as extrusion. injection. blow extrusion or rolling for example. They may be used advanta geously for applications where a good resistance to impact is required and in particular for manufacturing crates. tubs. pallets and bottles.

The examples which follow are intended to illustrate the invention and in no way restrict it.

EXAMPLES l to Magnesium ethylate, Mg(OC H titanium tetrabutylate, Ti(OnC H and ethyl aluminium dichloride Al(C H =,)Cl are reacted as follows:

114 g of magnesium ethylate was added to 170 g of titanium tetrabutylate and the mixture heated to 170C with agitation for 2V2 hours. There was almost complete dissolution of the magnesium ethylate. ln the mixture the atomic ratio of Ti/Mg was 0.5 gram atom/gram atom i error due to impurities contained by the reagents.

To the mixture thus made and previously cooled to ambient temperature there was added 400 mls of hexane at C and then. gradually. varying quantities of ethyl aluminium dichloride in the form of a solution in 10 autoclave was degassed and the polyethylene thus produced collected.

Table I shows the particular conditions for each experiment and also the results obtained. The ratio Al/Mg 5 Ti represents the number of moles of ethyl aluminium dichloride used per gram equivalent of magnesium and titanium present in the mixture. This ratio is also accurate to within l07(.

The results shown in Table I show that the productiv- 10 ity of the catalytic complexes (weight of polymer obtained per gram of complex used) and their specific activity (weight of polymer obtained per hour. per gram of transition metal used and per kg/cm of ethylene) vary according to the ratio Al/Mg Ti defined above.

15 They are maximum for values of this ratio of between 0.75 and 2 moles/gram equivalent.

TABLE 1 Ex. I Ex. 2 Ex. 3 Ex. 4 Ex. 5

Quantity of AI(C H =,)CI, used. g 159 318 635 879 I270 Al/Mg Ti ratio mole/g.-eq 0.3l 062 L 1.75 2.50 Elementary analysis of the catalytic complex magnesium mg/g 90 96 I05 88 29 titanium mglg 7o 92 I13 I H 202 aluminium mglg 48 4 l 36 49 chlorine mg/g 263 384 573 603 563 Specific surface area of the catalytic complex mlg l) 22 273 33'4 221 Quantity of catalytic complex used mg 27 l l 5 5 12 Quantity of polyethylene obtained g 32 as I38 I27 l2l Productivity gPE/g complex [200 5900 27.600 25.400 10.100 Specific activity gPE/hr X g Ti X kg/cm" C H H100 6400 24.400 22.300 5.000 Fluidity index of the PE gilt) mins tASTM Standard D 1238-57 T} 0.20 0.77 1.06 0.50 0.27

hexane containing 400 g/litre.

An exothermic reaction occurred with the formation of the catalytic complex in the form of a precipitate.

The catalytic complex thus formed was separated by filtration and washed with hexane. It was then dried in vacuo at 70C until its weight was constant.

Varying quantities of catalytic complex and 200 mg. of triisobutyl aluminium were introduced into a 1.5 -litre autoclave containing 0.5 litres of hexane. The temperature of the autoclave was then brought to about 85C. Ethylene was introduced under a partial pressure of IO kg/cm and hydrogen under a partial pressure of 4 kg/cm The polymerization was continued for 1 hour with agitation. maintaining the total pressure constant by the continuous addition of ethylene. After l hour the EXAMPLES 6 to 8 The catalytic complex was prepared as described for Examples 1 to 5. except that varying quantities of tita- 40 nium tetrabutylate and ethyl aluminium dichloride were used.

The polymerization was also carried out under the same conditions as in Examples l to 5.

Table 2 shows the particular conditions for each experiment as well as the results obtained.

TABLE 2 Ex. 6 Ex. 7 Ex. ll

Quantity of won-Cam. used g 85 340 680 Atomic ratio 'l'i/Mg g-atlgat 0.25 l 2 Quantity of AltC HgCl' used g (135 i270 2540 Ratio Al/Mg Ti mole/g-eq 1.66 1.66 2 Elementary analysis of the catalytic complex magnesium mg/g 104 23 titanium mg/g 76 I 2 l6 aluminium mg/g 43 3b 23 chlorine mg/g 6l6 5'93 495 Specific surface area of the catalytic complex m"/g 340 320 249 Quantity of catalytic complex used mg 4 5 6 Quantity of polyethylene obtained g l3l I30 66 Productivity gPe/g complex 32.800 26.000 1 1.000 Specific activity gPE/hr X g Ti X kg/em" C H. 43.000 15.750 5.l00 Fluidity index of the PE g/l0 mins 0.37 0.34 0.09

EXAMPLE 9 The same reagents as in Examples 1 to S were used. A mixture containing 100 mls. of hexane. 15 g ol'magnesium ethylate. and 4.5 g oftitanium tetrabutylate was maintained under agitation and at boiling point (approximately 69C) for 0.75 hours. ln this mixture the atomic ratio Ti/Mg was 0.10 gram atom/gram atom.

To the mixture thus obtained there was added 75 g of ethyl aluminium dichloride in the form ofa solution at the rate of 400 g/litre in hexane. This mixture was heated with agitation and under a reflux (approximately 73C) for 1 hour. The Al/Mg Ti ratio of the mixture was 2.10 moles/gram equivalent. A catalytic complex in the form of a precipitate was formed which was separated by filtration. It was then dried in vacuo at 70C until its weight remains constant.

The elemental analysis of the catalytic complex showed that it contained:

magnesium 219 mg/g titanium l4 mg/g aluminium 23 mg/g chlorine 703 mg/g Polymerization was carried out under conditions identical to those of Examples l to 5 using 21 mg of catalytic complex.

169 g of polyethylene were collected whose melt index was 0.15 g/l0 mins. The productivity was. therefore. 8000 gPE/g catalytic complex and the specific activity 57,500 g PE/hr. X g Ti X kg/cm C H EXAMPLE The same reagents were used as in Examples 1 to 5. except that the titanium tctrabutylate was replaced by titanium tetranonylate of the formula Ti(OC H 1 14 g of magnesium ethylate were added to 87 g of titanium tetranonylate. The mixture was heated to 195C with agitation for 2% hours. It was found that there is almost complete dissolution of the magnesium ethylate. 1n the mixture the Ti/Mg atomic ratio was 0.14 gram atoms/gram atom to within an error of I l07r due to impurities contained in the reagents.

To this mixture thus made and previously cooled to ambient temperature there was added 1600 mls. of hexane at C and then. gradually. 635 g of ethyl aluminium dichloride in the form of a 400 g/litre solution in hexane.

This mixture was heated with agitation and under a reflux (approximately 69C) for 0.75 hours. The Al/Mg Ti ratio of the mixture was 2 moles/gram equivalent. A catalytic complex in the form of a precipitate was formed. It was separated by filtration. washed with hexanc. and dried in vacuo at 70C until its weight remains constant.

The elemental analysis of the catalytic complex thus formed showed that it contained:

magnesium lhS trig/1.: titanium 41 mpg aluminium 45 inglg chlorine 641 mgrg A polymerization test was carried out under identical conditions to those of Examples 1 to 5 using 4 mg of catalytic complex.

144 g of polyethylene was recovered whose melt index is 1.09 g/lt) mins. The productivity was therefore 36.000 gPE/g catalytic complex and the specific activity was 88.000 gPE/hr. X g Ti X kg/em C H EXAMPLES 11 to 14 As in Examples 1 to 5. magnesium ethylate and ethyl aluminium dichloride were used but various derivatives of transition metal were used;

In Example I l. titanium tetraethylate-TitOC H in Example 12. vanadium oxyocty1ate-VO)OC, H

in Example 13. zirconium tetrabutylate-Zr(OC.H,.)

and

in Example 14. a condensed titanium butylate of the average formula:

This butylate is heated to 90C before being used.

114 g of magnesium ethylate was added to varying quantities of the above-mentioned transition metal derivatives. The mixture was heated to 170C accompanied by agitation for 2% hours and there was the almost complete dissolution of the magnesium ethylate.

After the mixture was cooled. 400 mls. of hexane at C were added to it and. gradually. varying quantities of ethyl aluminium dichloride in the form of a 400 g/litre solution in hexane.

An exothermic reaction was observed and the formation of a catalytic complex in the form of a precipitate.

The catalytic complex thus formed was separated by filtration. washed with hexane. and then dried in vacuo at C until its weight remains constant.

Polymerization tests were carried out under conditions identical to those of examples 1 to 5.

Table 3 shows the particular conditions for each test as well as the results obtained.

TABLE 3 Ex. 11 5x12 lix. 13 Ex. 14

Nature of the derivative of 'l'il0l-.t I, \"()(0()ct). Zr(()Bu). condensed transition metal Quantity of this derivative used g 114 573 383 253 Atomic ratio 'l'r/Mg L'fill/gill 0 5 l l 1 Quantity of All( |H lg used g n35 e35 (135 ms Ratio Al/Mg 'l'r mole/g-eq 1.25 0.71 0.83 0.83 lzlementar analysis of the catalytic complex magnesium mgfg 44 its so transition metal mg/g 10h ti l 181 128 aluminium mglg 34 73 29 3! chlorine mg/g 53! 7 480 408 TABLE 3 Continued Ex. ll lix. l2 Ex. l3 Ex. [-3

Spccil'ic surface area of the complex nr-Ig 343 [40 Quantity olcatalytic complex used g 5 IR 20 4 Quantity of polyethylene obtained g W7 84 6'. NH Productivity gPE/g complex 39t400 3.000 3.lll 26.000 Specific activity gPE/hr X g 'l'r kg/Ctti H 37.200 3.370 L700 20.300 Fluitlity index ol the PE 050 0.05 0.5l* 0.70

l-luidit index measured under hea\ load (2|.fi kg).

EXAMPLE l EXAMPLE l7 The same reagents were used as in Examples 1 to 5 plus zirconium tetrabutylate of formula Zr(OC H l 14 g of magnesium ethylate were mixed with 100 g of titanium tetrabutylatc and 153 g of zirconium tetrahutylate. The mixture was heated to l70C with agitation for 2 /2 hours and there was almost complete dissolution of the magnesium ethylate. In the mixture the Ti Zr/Mg atomic ratio was approximately 0.7 to within an error of i l07? due to impurities in the reagents. The Ti/Zr atomic ratio was approximately 0.75.

To the mixture thus prepared and previously cooled to ambient temperature there was added 400 mls. of hexane at C and then. gradually, 635 g of ethyl aluminium dichloride in the form of a 400 g/litre solution in hexane.

An exothermic reaction occurs with the formation of the catalytic complex in the form of a precipitate. The latter is separated by filtration and washed with hexane. It is then dried in vacuo at 70C until constant weight.

A polymerization test was carried out under conditions identical to those of Examples 1 to 5 except that the partial pressure of ethylene was 5 kg/cm and that of hydrogen 2 kg/cm" 6 mg of catalytic complex were used.

6t g of polyethylene were collected having a melt index of 0.44 g/lO mins. The productivity was. therefore. 10.000 gPE/g catalytic complex.

EXAMPLE 16 The catalytic complex was prepared as in Example 3 except that the ethyl aluminium dichloride there used was replaced by diethyl aluminium chloride Al(C H Cl.

The catalytic complex thus formed had the following elementary composition:

magnesium 67 mg/g titanium )2 mg/g aluminium )2 mg/g chlorine 385 mg/g A polymerization experiment was carried out as in Example 3. I47 g of polyethylene were collected with a melt index of l.34 g/l0 mins. The productivity was therefore 29.400 gPE/g complex and the specific activity was 32.000 gPE/hr X g Ti X kg/crn C .H

The catalytic complex was prepared as in Example 3 except that the ethyl aluminium dichloride was re placed by aluminium trichloride. The latter was used in the solid state in an amount of 665 g.

The catalytic complex thus formed had the following elemental composition:

magnesium 66 tug/g titanium l.(i mg/g 75 aluminium -16 mg/g chlorine 713 mgig A polymerization experiment was carried out as in Example 3 using I l mg of catalytic complex.

l7 g ofpolyethylene ofa melt index of0.08 g/l0 mins were collected. The productivity was therefore I500 gPE/g catalytic complex and the specific activity was 96.500 gPE/hr X g Ti lag/cm C .H

EXAMPLES l8 to 24 As in Examples l to 5. titanium tetrabutylatc and ethyl aluminium dichloride were used. However. in place of the magnesium ethylate there was used one of the following organic oxygenated compounds:

In Example l8. potassium ethylatc KOC H in Example l9. calcium ethylate Ca(OC H,-,)

in Example 20. zinc ethylate Zn(OC- .H

in Example 2l. aluminium propylate AI(OC;,H

in Example 22. silicon butylate Si(OC H,,)

in Example 23. manganese ethylate Mn(OC H and in Example 24, iron ethylate Fe(OC H Varying quantities of these organic oxygenated compounds were added to 340 g of titanium tetrabutylate. For the rest. the preparation of the catalytic complexes was carried out by the mode of operation described for Examples 1 to 5. The same applies to the polymeriza tion tests.

In order to carry out Example 22. a partially con densed silicon butylatc/titanium butylate complex of the commercial type as sold by Dynamit Nobel was used. This complex contained 84 g of titanium and 28 g of silicon per kg.

Table 4 shows the special conditions in each experiment as well as the results obtained.

TABLE 4 Ex. lR Ex. I) E\. 20 Ex. 2| Ex. 12 lix. 23 Ex. 14 Nature of the compound KOC H Ca(OC H ZnlOC- -H li AItOC HTM SilOlIXH MnlOC H-fl FClOCgHslzi Quantity of this compound used g M8 130 I 408 H5 l Atomic ratio Til Me ll-;ll g-1ll 0.5 l l 0.5 1.75 l l TABLE 4 Continued l;l\ IX Fx. 1! Ex. 20 Ex. Bl E\, I: :3 li\. 24

Nature ol the compound ROLE-H; CatOf H l Znl()( .H;,) ANOC- H I H,,) Y\lnI()L:H -,t C( -3Hf l;t

Quantity AIHL H-JCI used g (135 320 (135 1270 (13 635 635 Ratio AllMc Tl molc/g-cq 0.85 t] 40 ll 85 l 0.45 0.85 0.70

Elemcntary analysis of the catalytic complex Metal Me mg/g l3) l0l l-tt) [2 i117 Hi2 Titanium mg/g 83 129 l 38 209 239 NM '42 Aluminium mg/g 93 l7 3.) 74 44 I 7] Chlorine mg/g 623 378 393 Sl7 4l0 457 377 Specific surface area of the catalytic complex ni /g 74 it) 35 192 50 147 56 Quantity of catalytic complex used mg 30 22 2'4 ll 5! Quantity of polyethylene obtained g l8 77 25 as 70 55 93 Productivity gPE/g complex 600 3500 860 3500 2800 5000 I800 Specific activity gPE/hr x g Ti X lag/cm (:H; 700 2700 6200 1650 l I70 4760 2020 Fluidity index of the PE g/lO mins 0.08 1.4 010 0.1 l L99 0.63 [.08

*l-luidity index measured under heavy load (2 l .6 kg),

A ol merization test was carried out under condi- EXAMPLE 25 P y The same reagents were used as used in Examples l to 5 plus aluminium ethylatc of the formula Al- (OC2H5)3- l l4 g of magnesium ethylate were added to l44 g of titanium tetrabutylate mixed with 284 g of aluminium ethylate. The mixture was heated to 170C with agitation for 2 /2 hours and it was observed that there was almost complete dissolution of the magnesium ethylate. in the mixture the Ti/Mg Al atomic ratio was 0.15 gram atom/gram atom to within an error ofi 10% due to impurities contained by the reagents.

To the mixture thus made and previously cooled to ambient temperature there was added 400 mls. of hexane at 20C and then gradually 635 g of ethyl aluminium dichloride in the form of a 400 g per litre solution in hexane.

This mixture was heated with agitation and under a reflux (approx. 69C) for 0.75 hours. The Al/Mg Al Ti ratio of the mixture was approximately 0.60 moles/gram equivalent. A catalytic complex in the form of a precipitate was formed, separated by filtration. washed with hexane. and then dried in vacuo at 70C until its weight remains constant.

The elemental analysis of the complex thus formed shows that it contained:

magnesium 47 rng/g titanium 54 nig/g aluminium 92 mg/g chlorine 502 mg/g tions identical with those of Examples 1 to 5 using 7 mg of catalytic complex.

155 g of polyethylene were collected having a melt index of 3.04 g/lO mins. The productivity was. therefore. 22,200 gPE/g catalytic complex and the specific activity was 41.000 gPE/hr. X g Ti X kg/cm C H EXAMPLES 26 and 27 The following reagents were used:

magnesium ethylate Mg(OC H aluminium butylate AKOC H titanium tetranonylate Ti(OC ,H

ethyl aluminium dichloride Al(C H r,)Cl

l l4 g of magnesium ethylatc were added to 234 g of aluminium butylate mixed with varying quantities of titanium tetranonylate. The mixture was heated to 190C accompanied by agitation for 1% hours and it was observed that there was almost complete dissolution of the magnesium ethylate.

To the mixture thus formed and previously cooled to ambient temperature there was added 6 litres of hexane at 20C and then. gradually, 635 g of ethyl aluminium dichloride in the form of a 400 g per litre solution in hexane.

This mixture was heated to C with agitation for one hour resulting in the formation of a catalytic complcx in the form ofa precipitate. It was separated by filtration. washed with hexane, and then dried in vacuo at C until constant weight.

A polymerization test was carried out under conditions identical to those of Examples l to 5 except that only mg of triisobutyl aluminium were used.

Table 5 shows the special conditions for each experiment as well as the results obtained.

TABLE 5 Quantity of TKOC H used Atomic ratio 'li/Mg X Al gal/gal g ll TABLE Continued Ex. 20 Ex. 27

Elementary analysis of the catalytic complex magnesium mg/g 67 93 titanium mg/g I5 24 aluminium mg/g l l9 l3() chlorine nlg/g J79 43x Specific surface area of the catalytic complex m'-'/g Quantity of catalytic complex used mg 7.2 3.3 Quantity ol polyethylene obtained g I32 83 Productivity gPE/g complex 18.400 25.200 Specific activity gPE/hr X g Ti X kg/cni H, l22.ll00 [05.000 Fluidity index of the PE gill) mins L02 0.52

Examples 26 and 27 show that the specific activity is extremely high when the transition metal/metal ratio is between 0.025 and 0. l0 gram atom/gram atom.

EXAMPLES 28 to 32 The same reagents as used in Examples 1 to 5 were used except that the magnesium ethylate there used was replaced by:

In Example 28. magnesium phenate Mg(OC H in Example 29. magnesium formate Mg(OOCH) in Example 30. magnesium henzoate Mg(OOCC H in Example 3], magnesium hydroxymethylate and in Example 32. magnesium The catalytic complexes were prepared as in Examples l to 5 under the conditions stated in Table 6. except that l litre of hexane was used. A complete dissolution of the Ti(OC H did not result even after the addition of the hexane. On the contrary. a suspension of very fine particles was formed. to which there was added a solution of ethyl aluminium dichloride. Catalytic complexes were obtained analogous to those of the preceding examples. With each of these complexes a polymerization test was carried out under the conditions of Examples 1 to 5.

Table 6 shows the special conditions for each experiment and the results obtained.

acetylacetonate 76 g of polyethylene were collected having a melt index of 0.59 g/l0 mins. The productivity was. therefore. 7600 gPE/g complex and the specific activity was l0.000 gPE/hr. X g Ti X kg/cm C H EXAMPLE 34 The experiment carried out in Example l6 was reproduced except that 8 mg of the same catalyst were used and the 200 mg of triisobutyl aluminium were replaced by 120 mg of diethyl aluminium chloride.

6] g of polyethylene were recovered having a melt index of 0.08 g/l0 mins. The productivity was. therefore. 7600 gPE/g complex.

EXAMPLE 35 The same reagents were used as in Examples l to 5.

To 500 mls. of a solution of ethyl aluminium dichloride in hexane. at the rate of 400 g/litre. there was added successively l litre of hexane and 75 g of titanium tetrabutylate diluted in 100 mls. of hexane. The latter addition was carried out gradually. The temperature of the mixture rose at the end to about 35C. A precipitate was formed. 36 g of magnesium ethylate. in the solid state. were then added and the mixture was then heated to 60C with agitation for one hour.

The catalytic complex was filtered. washed with hexane. and then dried in vacuo at 70C until its weight remained constant.

The elemental analysis of the catalytic complex TABLE 6 Ex. 28 Ex. 29 Ex. 30 Ex. 3l Ex. 32

Nature of the compound Mgloc H h MglOOCH], m ioocctHo, MglOHlOCH, MglC;,H=O,), Quantity of this compound used g 2H) 57 I33 36 l ll Atomic ratio Ti/Me g-at/g-at 0.5 l l l 1 Quantity of Al(C H -,lCl, used g 635 318 3|? 3H1 3l8 Ratio Al/Me Ti mole/g-eq l.25 0.85 0.85 0.85 0.85 Elementary analysis ol the catalytic complex Magnesium mg/g 99 93 66 48 Titanium mg/g 92 I52 126 I67 97 Aluminium mg/g 39 I0 ll 27 I Chlorine mg/g 530 395 402 454 l6lt Specific surface area of the catalytic complex nf-lg Ill 24 149 Quantity of the catalytic complex used mg 5 7 7 12 32 Quantity of polyethylene obtained g 126 I57 60 1 [3 Productivity gPE/g complex 25.200 8.600 22.400 5.000 3.500 Specific activity gPE/hr X g 'l'i X Kg/cm H 7.400 5.530 17.500 3.050 3.600 Fluidity index of the PE g/ll) mins. 0.83 0.20 2.08 0.20 0.59

showed that is contained: EXAMPLE 33 The experiment carried out in Example I was repromagnesium 1H mg/g duced except that H) mg of the same catalytic complex tiwnipm 109 8's chlorine 393 mg/g were used and the 200 mg of triisobutyl aluminium were replaced by 72 mg of trimethyl aluminium.

Its specific surface area was l3: m lg.

A polymerization experiment was carried out under the same conditions as in Examples l to 5 except that I mg of triisobutyl aluminium were used. the partial pressures of ethylene and hydrogen were and 2 kg/cm respectively. and 7 mg of catalytic complex were used.

64 g of polyethylene were recovered having a melt index of 0.82 g/] 0 mins. The productivity amounted to 9100 gPE/g catalytic complex and the specific activity was l6.800 gPE/hr X g Ti X kg/cm" C H EXAMPLE 36 A catalytic complex prepared in accordance with Example 2 was used to copolymerize ethylene and propylene.

In a S-litrc autoclave there was placed successively 1.2 g of trihexyl aluminium and 2l75 mls. of propylene. It was heated to 40C whilst introducing ethylene until the total pressure amounted to l8.l kg/em 254 mg of catalytic complex were used.

The polymerization was continued for 6 hours with agitation at 40C.

At the end of the polymerization the autoclave was degassed and 384 g of an ethylene/propylene copolymer recovered containing 4] moles per cent of propylene.

EXAMPLE 37 A catalytic complex was prepared as in Examples 1 to 5 except that there was used. for l 14 g of magnesium ethylate. 680 g of titanium tctrabutylate and 635 g of ethyl aluminium dichloride. The Ti/Mg atomic ratio was. therefore. 2 gram atoms/gram atom to within an error of i I071. The Al/Mg Ti ratio was 0.5 moles/- gram equivalent to within l07r error.

The catalytic complex was used for a polymerization experiment carried out continuously in a 300-litrc reactor of the liquid-full" type provided with very effective agitation and cooling devices. The cooling device was regulated in such a way as to maintain the temperature in the reactor at 90C. The polymerization was carried out in suspension in hexane. The latter was introduced continuously into the reactor at the rate of 52 kg/hr.

There was also introduced:

I. Ethylene so as to maintain the concentration in the reactor at 4] g ethylene per kg. of diluent;

2. hydrogen so as to maintain the concentration in the reactor at 0.2l g of hydrogen per kg. of diluent; and

3. trimethyl aluminium so as to maintain the concentration in the reactor at 26 mg of ARCH per kg. of diluent.

The polymer suspension in the diluent was discharged so as to maintain the pressure in the reactor at 30 leg/cm".

6.8 kg of polyethylene per hour were recovered. This polyethylene possessed a density of 0.965 and a melt index of 5.1 g/lO mins. It only contained 2 ppm oftitanium originating from catalytic residues even though it did not undergo any purification.

Its Izod impact strength measured according to ASTM Standard D 256 was 10.5 kgcm/cm notch.

By way of comparison a similar polymerization test was carried out but using catalytic complex prepared in accordance with Example 3 of Belgian Pat. No. 767.586.

The special conditions of this comparative experiment were as follows:

rate of feed of hexane: 54.8 kg/hr.;

concentration of ethylene: 34 g/kg. of diluent;

concentration of hydrogen: 0.26 g/kg of diluent; and

concentration of AI(CH;,)=,: 17 mg/kg of diluent.

6.7 kg of polyethylene per hour were recovered. This polyethylene had a density of0.965 and a melt index of 5.8 g/lt) mins. It contained 3 ppm oftitanium. Its Izod impact strength was only 6.4 kg cm/cm notch.

It will be seen that the catalytic complexes according to the invention make it possible to obtain. with still further improved catalytic activities. polymers which for more or less equivalent melt indices have an Izod impact strength which is distinctly greater than that of the best polymers according to prior art.

It will be understood that it is intended to cover all changes and modifications of the examples of the invention herein chosen for the purpose of illustration which do not constitute departures from the spirit and scope of the invention.

What is claimed is:

I. A process for the polymerization and eopolymerization of a-olefins which comprises conducting the polymerization or eopolymerization in the presence of a catalyst composition comprising A. the solid reaction product of l at least one nonhalide containing organic oxygenated compound of a metal selected from the metals of Groups la. Ila. Ilb. lllb. IVb. Vlla. and VIII of the Periodic Table, with (2) at least one non-halide containing organic oxygenated transition compound of a transition metal selected from the metals of Groups lVa, Va. and Vla of the Periodic Table. and with (3) an organo aluminum halide having the general formula AIR R' in which R is a hydrocarbon radical containing l to 20 carbon atoms. R is a halide and n is any number such that l 5 n s 2'. and

B. an organo-metallic compound selected from the organic derivatives of metals of Groups Ia, Ila. Uh. [11b and IVb of the Periodic Table.

2. The process of claim I wherein the metal of compound (l is lithium. sodium, potassium. maagnesium. calcium. zinc. boron. aluminum. silicon. manganese. iron. nickel. cobalt. or tin; and the transition metal is titanium, zirconium. or vanadium.

3. The process of claim 2 wherein the metal is magnesium the transition metal is titanium. and the halide is a chloride.

4. The process of claim I wherein two organic oxygenated compounds are used; one of a metal of Group Ila of the Periodic Table and the other a metal of Group "lb or IVb of the Periodic Table.

5. The process ofelaim 4 wherein the metal of Group Ila is magnesium and the metal of Groups Illb or IVb is aluminium or silicon.

6. The process of claim 1 wherein the organic oxygenated compound is an alkoxide. phenate. salt of a carboxylic acid. an enolate. an oximate. salt of a hydroxamic acid. or salt of a hydroxylamine'. the organic oxygenated transition compound is an alkoxide. oxyalkoxide. condensed alkoxidc or enolate; and the aluminum halide has the general formula AIR,,R'; in which R is a C, to C r, alkyl. cycloalkyl. arylalkyl. aryl. or alkylaryl radical. and R is chlorine.

7. The process of claim 1 wherein the atomic ratio oi transition metal present in the organic oxygenated transition compound to metal present in the organic oxy- 21 genated compound used in making the complex is between (HH and l gram atoms per gram atom.

8. The process ofclaim 7 including an amount ofaluminium halide present in preparing the complex such that the ratio between the amount of Al and said metal and transition metal. Al/metal transition metal. is between 0.0l and moles/gram equivalent.

9. The process of claim I wherein the organic oxygenatcd compound l is selected from the group consisting of magnesium alkoxide and magnesium phenate in which the hydrocarbon radical contains from 1 to 6 carbon atoms; the organic oxygenated transition compound (2) is a titanium alkoxide in which the hydrocarbon radical contains from I to 10 carbon atoms; the aluminum halide (3) has the general formula AlR,,R in which R is an alkyl radical containing from I to 6 carbon atoms. R is chlorine and n 2; the ratio of Ti/Mg is between 0.025 and 2; and the ratio Al/Mg-t-Ti is between 0.50 and 5 moles/gram equivalent.

l0. The process of claim 9 wherein the ratio ofTi/Mg is between 0.1 and 2 and the ratio of Al/Mg-l-Ti is be tween 0.75 and 2.

H. A process for the polymerization and copolymerization of a-olefins in the presence of a catalytic composition comprising A. the solid reaction product of l at least one organic oxygenated compound selected from bivalent metal alkoxides and bivalent metal phenates which possess only sequences of divalent metaloxygen-organic radical bonds. with (2) at least one non-halide containing organic oxygenated transition compound of a transition metal selected from the metals of Groups lVa. Va. and Vla of the Periodic Table and with (3) an organo-aluminum hal- 22 ide compound having the general formula AlR,,R in which R is a hydrocarbon radical containing 1 to 20 carbon atoms. R' is a halide and n is any number such that l s n s 2; and

B. an organometallic compound selected from the organic derivatives of metals of Groups la. lla. llb. lllb. and Nb of the Periodic Table.

I2. The process of claim ll wherein the bivalent metal is magnesium. the transition metal is titanium and the halide is a chloride.

13. The process of claim ll wherein the atomic ratio of transistion metal present in the organic oxygenated transition compound to bivalent metal present in the organic oxygenated compound used in making the complex is between 0.0l and [0 gram atoms per gram atom.

M. The process ol'claim ll wherein the organic oxygenated compounds are selected from the group consisting of magnesium alkoxide and magnesium phe nates in which the hydrocarbon radical contains from I to 6 carbon atoms; the organic oxygenated transition compound is a titanium alkoxide in which the hydrocarbon radical contains from I to 10 carbon atoms; the aluminum halide has the general formula of AIR,,R in which R is an alkyl radical containing l to 6 carbon atoms, R is a chloride and n 2; the ratio of titanium/- magnesium is between 0.25 and 2; and the ratio of aluminum/magnesium titanium is between 0.50 and 5 moles/gram equivalent.

15. The process of claim 11 wherein the ratio of titanium/magnesium is between 0.] and 2 and the ratio of Al/Mg Ti is between 0.75 and 2. 

1. A PROCESS FOR THE POLYMERIZATION AND COPOLYMERIZATION OF A-OLEFINS WHICH COMPRISES CONDUCTING THE POLYMERIZATION OR COPOLYMERIZATION IN THE PRESENCE OF A CATAYST COMPOSITIOM COMPRISING A. THE SOLID REACTION PRODUCT OF (1) AT LEAST ONE NON-HALIDE CONTAINING ORGANIC OXYGENATED COMPOUND OF A METAL SELECTED FROM THE METALS OF GROUPS IA, IIA, IIB, IIIB, IVB, VIIA, AND VIII OF THE PERIODIC TABLE, WITH (2) AT LEAST ONE NON-HALIDE CONTAINING ORGANIC OXYGENATED TRANSITON COMPOUND OF A TRANSITION METAL SELECTED FROM THE METALS OF GROUPS IVA, VA, AND V1A OF THE PERIODIC TABLE, AND WITH (3) AN ORGANO ALUMINUM HALIDE HAVING THE GENERAL FORMULA A1RNR'' 3-N UN WHICH R IS A HYDROCARBON RADICAL CONTAINING 1 TO 20 CARBON ATOMS, R'' IS A HALIDE AND N IS ANY NUMBER SUCH THAT 1 N 2: AND B. AN ORGANO-METALLIC COMPOUND SELECTED FROM THE ORGANIC DERIVATIVES OF METALS OF GROUPS IA, IIB, IIB, IIIB AND IVB OF THE PERIIODIC TABLE.
 2. The process of claim 1 wherein the metal of compound (1) is lithium, sodium, potassium, maagnesium, calcium, zinc, boron, aluminum, silicon, manganese, iron, nickel, cobalT, or tin; and the transition metal is titanium, zirconium, or vanadium.
 3. The process of claim 2 wherein the metal is magnesium the transition metal is titanium, and the halide is a chloride.
 4. The process of claim 1 wherein two organic oxygenated compounds are used; one of a metal of Group IIa of the Periodic Table and the other a metal of Group IIIb or IVb of the Periodic Table.
 5. The process of claim 4 wherein the metal of Group IIa is magnesium and the metal of Groups IIIb or IVb is aluminium or silicon.
 6. The process of claim 1 wherein the organic oxygenated compound is an alkoxide, phenate, salt of a carboxylic acid, an enolate, an oximate, salt of a hydroxamic acid, or salt of a hydroxylamine; the organic oxygenated transition compound is an alkoxide, oxyalkoxide, condensed alkoxide or enolate; and the aluminum halide has the general formula AlRnR''3-n in which R is a C1 to C20 alkyl, cycloalkyl, arylalkyl, aryl, or alkylaryl radical, and R'' is chlorine.
 7. The process of claim 1 wherein the atomic ratio of transition metal present in the organic oxygenated transition compound to metal present in the organic oxygenated compound used in making the complex is between 0.01 and 10 gram atoms per gram atom.
 8. The process of claim 7 including an amount of aluminium halide present in preparing the complex such that the ratio between the amount of Al and said metal and transition metal, Al/metal + transition metal, is between 0.01 and 10 moles/gram equivalent.
 9. The process of claim 1 wherein the organic oxygenated compound (1) is selected from the group consisting of magnesium alkoxide and magnesium phenate in which the hydrocarbon radical contains from 1 to 6 carbon atoms; the organic oxygenated transition compound (2) is a titanium alkoxide in which the hydrocarbon radical contains from 1 to 10 carbon atoms; the aluminum halide (3) has the general formula AlRnR''3-n in which R is an alkyl radical containing from 1 to 6 carbon atoms, R'' is chlorine and n 2; the ratio of Ti/Mg is between 0.025 and 2; and the ratio Al/Mg+Ti is between 0.50 and 5 moles/gram equivalent.
 10. The process of claim 9 wherein the ratio of Ti/Mg is between 0.1 and 2 and the ratio of Al/Mg+Ti is between 0.75 and
 2. 11. A process for the polymerization and copolymerization of Alpha -olefins in the presence of a catalytic composition comprising A. the solid reaction product of (1) at least one organic oxygenated compound selected from bivalent metal alkoxides and bivalent metal phenates which possess only sequences of divalent metal-oxygen-organic radical bonds, with (2) at least one non-halide containing organic oxygenated transition compound of a transition metal selected from the metals of Groups IVa, Va, and VIa of the Periodic Table and with (3) an organo-aluminum halide compound having the general formula AlRnR''3-n in which R is a hydrocarbon radical containing 1 to 20 carbon atoms, R'' is a halide and n is any number such that 1 < or = n < or = 2; and B. an organometallic compound selected from the organic derivatives of metals of Groups Ia, IIa, IIb, IIIb, and IVb of the Periodic Table.
 12. The process of claim 11 wherein the bivalent metal is magnesium, the transition metal is titanium and the halide is a chloride.
 13. The process of claim 11 wherein the atomic ratio of transistion metal present in the organic oxygenated transition compound to bivalent metal present in the organic oxygenated compound used in making the complex is between 0.01 and 10 gram atoms per gram atom.
 14. The process of claim 11 wherein the organIc oxygenated compounds are selected from the group consisting of magnesium alkoxide and magnesium phenates in which the hydrocarbon radical contains from 1 to 6 carbon atoms; the organic oxygenated transition compound is a titanium alkoxide in which the hydrocarbon radical contains from 1 to 10 carbon atoms; the aluminum halide has the general formula of AlRnR''3-n in which R is an alkyl radical containing 1 to 6 carbon atoms, R'' is a chloride and n 2; the ratio of titanium/magnesium is between 0.25 and 2; and the ratio of aluminum/magnesium + titanium is between 0.50 and 5 moles/gram equivalent.
 15. The process of claim 11 wherein the ratio of titanium/magnesium is between 0.1 and 2 and the ratio of Al/Mg + Ti is between 0.75 and
 2. 